CN201261759Y - Apparatus for preparing ultra-high molecular weight polyacrylamide by posthydrolysis - Google Patents
Apparatus for preparing ultra-high molecular weight polyacrylamide by posthydrolysis Download PDFInfo
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- CN201261759Y CN201261759Y CNU2008200805250U CN200820080525U CN201261759Y CN 201261759 Y CN201261759 Y CN 201261759Y CN U2008200805250 U CNU2008200805250 U CN U2008200805250U CN 200820080525 U CN200820080525 U CN 200820080525U CN 201261759 Y CN201261759 Y CN 201261759Y
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- single screw
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- screw pelletizer
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Abstract
The utility model relates to a device used for preparing super-high molecular weight polyacry lamide in a hydrolysis method. The discharge hole of a polymeric kettle is connected with the feeding hole of a first single-screw pelletizer; a conveyor belt or a stainless steel tank with an angle of inclination are mounted below the discharge hole of the first single-screw pelletizer; one end of the conveyor belt or the stainless steel tank is connected with the feeding hole of a single-screw blender; the feeding hole of the single-screw blender is respectively connected with the discharge hole of a vibratory dry powder feeder and the discharge hole of a stainless storage tank through a pipe line; the discharge hole of the single-screw blender is connected with the feeding hole of a intermediate bunker directly; the discharge hole of the intermediate bunker is directly connected with the feeding hole of a second single-screw pelletizer; and the discharge hole of the second single-screw pelletizer is connected with the feeding hole of a dryer through the pipe line. The utility model ensures that a continuous production of first pelleting, hydrolysis and second pelleting are realized; the energy consumption is utilized, so as to help to stabilize the quality of products; and the production efficiency is improved more than half a double.
Description
Technical field
The utility model belongs to the equipment of suitability for industrialized production polyacrylamide, is applicable to that particularly the posthydrolysis method prepares the equipment of super high molecular weight polyacrylamide.
Technical background
Before having, present domestic high molecular weight polyacrylamide suitability for industrialized production method commonly used adds alkali cohydrolysis and homopolymerization posthydrolysis.Before to add the alkali cohydrolysis be before the monomer acrylamide polymerization the required alkali of hydrolysis to be added in the polymerization system, after polymerization is finished system is warmed up to more than 80 ℃, insulation makes the polymkeric substance hydrolysis more than 2 hours, the granulation oven dry obtains product then.Before to add the alkali cohydrolysis method simpler, the equipment less investment, a lot of medium-sized and small enterprises all make in this way.But before add the alkali cohydrolysis since polymerization before alkali is added, reduced on the one hand colloidal effective content after the polymerization, add before the polymerization on the other hand a large amount of alkali raise system the pH value and may introduce a large amount of impurity, influence initiated polymerization efficient, for polymerization must add a large amount of initiators fully, therefore the products therefrom molecular weight is relatively low, generally is lower than 2,000 ten thousand.Expect super high molecular weight polyacrylamide, under present working condition, must adopt homopolymerization posthydrolysis method.Homopolymerization posthydrolysis suitability for industrialized production polyacrylamide comprises after the granulation, granulation of monomeric polymerization, polymeric colloid according to service requirements and carries out carrying out secondary granulation drying and crushing packaging final prod then after in various degree the hydrolysis, hydrolysis.Required equipment comprises polymerization unit, granulating equipment, hydrolysis device and drying plant.Be specially polymeric kettle below by about 5 meters long pipe connection to dual-screw pelletizer; dual-screw pelletizer links to each other with high-power blower; pipe connection by being about the about 15cm of 5 rice diameters is to large-scale hydrolysis device ager then; the ager lower end links to each other with intermediate bunker; order screw pelletizer under the intermediate bunker is connected with drying plant by travelling belt then.The production operation process is that polyacrylamide colloid carries out a granulation through dual-screw pelletizer at polymeric kettle after long pipeline is extruded; blow in the hydrolysis device of eminence by high-power blower then; in hydrolysis device, add alkali and hydrolysis auxiliary agent; be heated to the temperature required hydrolysis reaction (being generally 2 hours) that carries out certain hour; colloidal solid after the hydrolysis enters intermediate bunker; carry out secondary granulation through coupled single screw pelletizer, enter the drying plant drying by travelling belt then.There are several shortcomings in this traditional production method, first connect below the polymeric kettle be about 5 meters pipeline increased polymerization greatly after the required pressure of colloid discharging, limited discharging speed, second because hydrolytic process is used large-scale hydrolysis device, must blow in the hydrolysis device by blower fan after causing colloid through granulation for the first time, this has consumed a large amount of electric energy on the one hand, has reduced the temperature of colloid self on the other hand, colloid also needs reheat in hydrolytic process, this has consumed portion of energy again; The 3rd, it is thinner usually to blow the colloidal pipeline in hydrolysis device, if discharging speed is very fast, is easy to cause the obstruction of pipeline, increases discharging time; The 4th, colloid is to carry out after with the whole granulations of the colloid in the reactor through the hydrolysis device hydrolysis, and this time is grown (more than 2 hours) usually, and a large amount of colloids is difficult to mix in the alkaline hydrolysis process simultaneously, cause product hydrolysis degree heterogeneity, influence solubility property.Find out by above-mentioned, the defective that exists in the existing super high molecular weight polyacrylamide production method, during as production charges, energy consumption is big, the while unstable product quality, the different time sections product exists degree of hydrolysis and deliquescent difference etc., is because the equipment of preparation super high molecular weight polyacrylamide exists obvious structure design defective to cause.
Summary of the invention
The purpose of this utility model is in order to overcome above-mentioned because production and the product problem that the defective of production unit is brought, existing installation is improved, provide a kind of equipment that the posthydrolysis method prepares super high molecular weight polyacrylamide that is used for, to realize the continuous production of a granulation-hydrolysis-secondary granulation.Enhance productivity, cut down the consumption of energy, help stabilized product quality.
Equipment of the present utility model be avoid the colloid granulation after blower fan when blowing to eminence caused energy expenditure, colloid cooling, time waste, hydrolytic reagent mix energy expenditure inhomogeneous and the hydrolysis heating with colloid; in existing equipment, the long pipeline that will link to each other with polymeric kettle, large-scale hydrolysis device and incidental blower fan thereof blow equipment, dual-screw pelletizer removes or replace.Be used for the equipment that the posthydrolysis method prepares super high molecular weight polyacrylamide and comprise polymeric kettle through improved, first single screw pelletizer, travelling belt or have the stainless steel tank at angle of inclination, vibration dry powder feeder, stainless steel storage tank, single screw rod blender, intermediate bunker, second single screw pelletizer and moisture eliminator etc.;
The discharge port of polymeric kettle directly is connected with the opening for feed of first single screw pelletizer, the discharge port below of first single screw pelletizer is equipped with travelling belt or has the stainless steel tank at angle of inclination, travelling belt or have the end of stainless steel tank at angle of inclination and the opening for feed of single screw rod blender joins, the opening for feed of single screw rod blender also is connected with the discharge port of vibration dry powder feeder and the discharge port of stainless steel storage tank by pipeline respectively; The discharge port of single screw rod blender directly is connected with the opening for feed of intermediate bunker, and the discharge port of intermediate bunker directly is connected with the opening for feed of second single screw pelletizer, and the discharge port of second single screw pelletizer is connected with the opening for feed of moisture eliminator by pipeline.
Described polymeric kettle is more than one.
Equipment of the present utility model is when work; monomer solution is finished polymerization in polymeric kettle after; pressurization is extruded; first single screw pelletizer through linking to each other with polymeric kettle carries out a granulation, and (this first single screw pelletizer can be shared for more than one polymeric kettle; many stills are shared to be moved between polymeric kettle by the tablets press glide path); colloid after a granulation enters single screw rod blender; with vibration dry powder feeder and effusive hydrolysis auxiliary agent of stainless steel storage tank and hydrolysis alkali short mix; colloid enters intermediate bunker and utilizes the temperature of colloid self to be hydrolyzed then; hydrolysis is after secondary granulation enters drying plant, the dry packing finished product.
The obvious benefit of equipment of the present utility model has the following aspects: 1) removed the long pipeline that links to each other with polymeric kettle, reduced discharging pressure, improved discharging speed; 2) colloid does not need to blow through blower fan after a granulation, the line clogging problem can not occur, and discharging speed is unrestricted, increases substantially production efficiency, has reduced the electric energy loss of large fan simultaneously; 3) equipment of the present utility model has removed large-scale hydrolysis device, has reduced the equipment input, reduces the required heating of hydrolysis device significantly and stirs energy consumption; 4) avoided to a certain extent owing to a large amount of mixing difficulty of colloid in adding the alkali process, the inhomogenous shortcoming of product hydrolysis degree helps hydrolysis auxiliary agent and colloid and mixes, and helps stabilized product quality; 5) polymkeric substance discharging, granulation and hydrolytic process become serialization substantially, and efficiency of equipment is enhanced about more than once.
Below in conjunction with accompanying drawing the utility model is further described.
Description of drawings
Fig. 1. the utility model equipment synoptic diagram.
Reference numeral
1. polymeric kettle 2. first single screw pelletizers
3. travelling belt or have the stainless steel tank 4. vibration dry powder feeders at angle of inclination
5. stainless steel storage tank 6. single screw rod blenders
7. intermediate bunker 8. second single screw pelletizers
9. moisture eliminator
Embodiment
See also Fig. 1.The equipment of preparation super high molecular weight polyacrylamide of the present utility model comprises polymeric kettle 1, first single screw pelletizer 2, travelling belt or have the stainless steel tank 3 at angle of inclination, vibration dry powder feeder 4, stainless steel storage tank 5, single screw rod blender 6, intermediate bunker 7, second single screw pelletizer 8, moisture eliminator 9 etc.;
The discharge port of the polymeric kettle 1 of 3 parallel connections directly is connected with the opening for feed of first single screw pelletizer 2 of 1 meter long, the discharge port below of first single screw pelletizer 2 is equipped with travelling belt or has the stainless steel tank 3 at angle of inclination, the discharge port of the vibration dry powder feeder 4 that travelling belt or have the end of stainless steel tank 3 at angle of inclination and the opening for feed of single screw rod blender 6 joins, the opening for feed of single screw rod blender 6 are also installed by pipeline and its top respectively and the discharge port of stainless steel storage tank 5 are connected; The discharge port of single screw rod blender 6 directly is connected with the opening for feed of intermediate bunker 7 below it; the discharge port of intermediate bunker 7 directly is connected with the opening for feed of second single screw pelletizer 8 below it, and the discharge port of second single screw pelletizer 8 is connected by the opening for feed of pipeline with moisture eliminator 9.
Acrylamide monomer is after the polymeric kettle polymerization is finished; the colloid temperature is greater than 70 ℃; be a granulated into＜colloidal solid of 5mm through first single screw pelletizer; colloidal solid is transported to single screw rod blender through travelling belt or stainless steel tank with angle of inclination; temperature does not almost reduce; vibration dry powder feeder (containing the hydrolysis auxiliary agent) by single screw rod blender top; stainless steel storage tank (containing alkali lye); press quantitative adding alkali of discharging speed and hydrolysis auxiliary agent; like this colloidal solid by single screw rod blender fast with alkali and hydrolysis auxiliary agent mixing; enter into intermediate bunker then and be hydrolyzed, enter drying plant through second single screw pelletizer granulation again.Compare with the hydrolysis of being undertaken by hydrolysis devices such as agers in the past, every still product (identical output) can be saved time about 5 hours, and had saved a large amount of energy consumptions, can obtain molecular weight and be about 23,000,000 polyacrylamide.
Claims (2)
1. one kind is used for the equipment that the posthydrolysis method prepares super high molecular weight polyacrylamide, comprise polymeric kettle, first single screw pelletizer, travelling belt or have the stainless steel tank at angle of inclination, vibration dry powder feeder, stainless steel storage tank, single screw rod blender, intermediate bunker, second single screw pelletizer and the moisture eliminator; It is characterized in that:
The discharge port of polymeric kettle directly is connected with the opening for feed of first single screw pelletizer, the discharge port below of first single screw pelletizer is equipped with travelling belt or has the stainless steel tank at angle of inclination, travelling belt or have the end of stainless steel tank at angle of inclination and the opening for feed of single screw rod blender joins, the opening for feed of single screw rod blender also is connected with the discharge port of vibration dry powder feeder and the discharge port of stainless steel storage tank by pipeline respectively; The discharge port of single screw rod blender directly is connected with the opening for feed of intermediate bunker, and the discharge port of intermediate bunker directly is connected with the opening for feed of second single screw pelletizer, and the discharge port of second single screw pelletizer is connected with the opening for feed of moisture eliminator by pipeline.
2. according to claim 1ly be used for the equipment that the posthydrolysis method prepares super high molecular weight polyacrylamide, it is characterized in that: described polymeric kettle is more than one.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200805250U CN201261759Y (en) | 2008-05-13 | 2008-05-13 | Apparatus for preparing ultra-high molecular weight polyacrylamide by posthydrolysis |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200805250U CN201261759Y (en) | 2008-05-13 | 2008-05-13 | Apparatus for preparing ultra-high molecular weight polyacrylamide by posthydrolysis |
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| Publication Number | Publication Date |
|---|---|
| CN201261759Y true CN201261759Y (en) | 2009-06-24 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2008200805250U Expired - Lifetime CN201261759Y (en) | 2008-05-13 | 2008-05-13 | Apparatus for preparing ultra-high molecular weight polyacrylamide by posthydrolysis |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102060965B (en) * | 2009-11-11 | 2012-07-04 | 中国科学院理化技术研究所 | Preparation method of partially hydrolyzed polyacrylamide with improved temperature and salt resisting performances |
| CN106669523A (en) * | 2017-01-17 | 2017-05-17 | 山东宝莫生物化工股份有限公司 | Continuous conveying mixer for polyacrylamide colloidal particles |
| CN112679632A (en) * | 2020-12-25 | 2021-04-20 | 东营宝莫环境工程有限公司 | Novel efficient mixed hydrolysis method for producing polyacrylamide |
-
2008
- 2008-05-13 CN CNU2008200805250U patent/CN201261759Y/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102060965B (en) * | 2009-11-11 | 2012-07-04 | 中国科学院理化技术研究所 | Preparation method of partially hydrolyzed polyacrylamide with improved temperature and salt resisting performances |
| CN106669523A (en) * | 2017-01-17 | 2017-05-17 | 山东宝莫生物化工股份有限公司 | Continuous conveying mixer for polyacrylamide colloidal particles |
| CN112679632A (en) * | 2020-12-25 | 2021-04-20 | 东营宝莫环境工程有限公司 | Novel efficient mixed hydrolysis method for producing polyacrylamide |
| CN112679632B (en) * | 2020-12-25 | 2022-12-06 | 东营宝莫环境工程有限公司 | Efficient mixed hydrolysis method for producing polyacrylamide |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20090624 |
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| CX01 | Expiry of patent term |